CN103619830B - Liquid phase acid catalyst is used to manufacture cyclic acetal or ketal - Google Patents
Liquid phase acid catalyst is used to manufacture cyclic acetal or ketal Download PDFInfo
- Publication number
- CN103619830B CN103619830B CN201280030098.4A CN201280030098A CN103619830B CN 103619830 B CN103619830 B CN 103619830B CN 201280030098 A CN201280030098 A CN 201280030098A CN 103619830 B CN103619830 B CN 103619830B
- Authority
- CN
- China
- Prior art keywords
- acid
- reactor
- compound
- polyol
- cyclic
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D317/00—Heterocyclic compounds containing five-membered rings having two oxygen atoms as the only ring hetero atoms
- C07D317/08—Heterocyclic compounds containing five-membered rings having two oxygen atoms as the only ring hetero atoms having the hetero atoms in positions 1 and 3
- C07D317/10—Heterocyclic compounds containing five-membered rings having two oxygen atoms as the only ring hetero atoms having the hetero atoms in positions 1 and 3 not condensed with other rings
- C07D317/12—Heterocyclic compounds containing five-membered rings having two oxygen atoms as the only ring hetero atoms having the hetero atoms in positions 1 and 3 not condensed with other rings with only hydrogen atoms or radicals containing only hydrogen and carbon atoms, directly attached to ring carbon atoms
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Manufacture cyclic compound, such as cyclic acetal or the method for cyclic ketone: under the polyol of at least 3:1 with the mol ratio of aldehydes or ketones compound, aldehydes or ketones compound and polyol are supplied to reactor, these compounds are made to react to generate the even in liquid phase reactant mixture containing this acid catalyst in the presence of homogeneous acid catalyst, from reactant mixture, water is separated when forming water the most in the reactive mixture, from reactor, even in liquid phase reactant mixture is taken out as liquid product stream, and liquid reacting product stream is supplied to distillation column to be separated with unreacted polyol by cyclic acetal compounds, optionally unreacted polyol and/or acid catalyst are recirculated back to reactor.The method manufactures cyclic acetal compounds with high yield.The method also is adapted for being manufactured cyclic ketal by ketonic compound.
Description
1. Invention field
The present invention relates to manufacture cyclic acetal or ketal with high yield.
2. Background of invention
Ether alcohol, such as butoxy ethanol, has important industrial function in the product of cleaning supplies and coating etc.Cross
Go, the manufacture method based on the reaction relied between alcohol and oxirane of these products.This traditional method is verified a little
Poor efficiency, because it produces various unacceptable by-product together with ether alcohol.
Can also in acid condition reaction between aliphatic aldehydes and ethylene glycol (replacement oxirane) (ring-type to produce
Acetal) middle manufacture monoether glycol.Such as Hibbert and Timm (Hibbert, H.；Timm, J.A.J. Am. Chem. Soc. 1924, 46(5), 1283-1290) describe ethylene glycol and the acetal of butyraldehyde and obtain with the maximum yield of 50%.This
A little cyclic acetals or when ketone substitutes this aldehyde, ketal can stand hydrogenolysis subsequently in the presence of palladium and phosphoric acid catalyst.Special in the U.S.
Profit No. 4,484,009 describes this method.
Polyol is to there is acetal product and the balancing response of water by-product with the reaction of aldehydes or ketones.Water byproduct
Acetal is hydrolyzed reduction acetal or the yield of ketal.Therefore, it is intended that remove water from reaction system to improve the yield of acetal.
It is difficult for separating water from reactant mixture because its generally with aldehyde reaction thing and with the formation of cyclic acetal product
Azeotropic mixture.Entrainer has been used to pass through azeotropic distillation except water.Sulzbacher and colleague such as describe the many at ethylene glycol
The preparation process of acetal use benzene except water (Sulzbacher, M. et al.J. Am. Chem. Soc. 1948,70(8),
2827-2828).The environment of benzene and health effect are the obvious problems in this method.Desiccant can be used in the reactor,
Such as calcium chloride (DE 419223；Br nsted and GroveJ. Am. Chem. Soc. 1930, 52(4), 1394-1403)
Remove water when water is formed, but the throwing aside of solid waste generated is economy and environmental problem.
As the other method described in Astle and colleague relates to heating two alcohols and aldehydes on heterogeneous acidic resins and forming contracting
Distillate when aldehyde and water they (Astle, M.J. et al.,Ind. Eng. Chem. 1954¸46(4), 787-791).This side
Method is generally of low yield, and an example of butoxy ethanol manufacture is reported as using the ethylene glycol of about 1.3:1: butyraldehyde
Mol ratio has the yield of about 92%.In these react, flask separates from reactant mixture when forming water water,
In the completed, the reactant mixture in flask filtered and be separated.Under following except water from reactant mixture when forming water
State understanding: polyol is the balancing response that there is product acetal and water byproduct with the reaction of aldehyde, and water byproduct is to contracting
The hydrolysis of aldehyde reduces the yield of acetal or when forming water except water can improve the yield of acetal.
It has also been reported that a cooking-pot type response system, i.e. make aldehyde and polyhydroxy direct with hydrogen in the presence of noble metal catalyst
React into required ether alcohol.Such as, United States Patent (USP) No. 5,446,210 describe in a cooking-pot type system by making polyhydroxy and aldehyde
Reacting, with hydrogen, the method manufacturing hydroxy ether hydrocarbon in the presence of noble metal catalyst, wherein polyhydroxy with the mol ratio of aldehyde compound is
5:1 to 1:5, but under these mol ratios, when including monoether product is had low selective two kinds of by-product, receive
Rate low 35 to 50%.
U.S. Publication No. 2010/0048940 also illustrates a cooking-pot type system, and wherein polyhydroxy and aldehyde compound and hydrogen exist
In the presence of hydrogenolysis catalyst, one reacts to provide polyhydroxy ethers, wherein the mol ratio of polyhydroxy and aldehyde more than 5:1 to improve choosing
Selecting property and yield.Report an example of two step method, first synthesize acetal compound, then impose hydrogenolysis, do not retouch
State the yield value of the acetal made, although by acetal hydrogenolysis generate butoxy ethanol it is reported have about 61% selection
Property.
In the United States Patent (USP) 5917059 authorizing BASF Aktiengesellschaft, author is by making molar excess
Aldehyde and ketone react generation cyclic acetal and ketal in presence of an acid catalyst with polyol.Remove water as follows: evaporate continuously
Going out unreacted aldehydes or ketones raw material, water that thus condistillation is formed in water/aldehyde azeotropic mixture also replaces with fresh aldehydes or ketones further
The aldehydes or ketones that generation distillates.Aldehyde and ketone act not only as reactant, act also as the medium for carrying the water generated in reaction.This side
Method needs aldehyde (aldehyde of such as 4:1: alcohol mol ratio) the ability success of a large amount of excess.
Reactive distillation is used to generate low boiling contracting in United States Patent (USP) 6,015,875 and United States Patent (USP) 7,534,922 B2
Aldehyde.Author utilizes heterogeneous acid feeding low boiling raw material in column packing, such as methanol, ethanol, formaldehyde and acetaldehyde.Anti-in distillation
Tower top above district is answered to remove the acetal formed and remove water byproduct below distillation reaction district.This method is by available reactant
Type be limited to produce those of material of boiling at a temperature of lower than water.
Can be seen that from obtaining document, it is still desirable to use simple economic means with high yield manufacture cyclic acetal or
Ketal compound.
3. Summary of the invention
Can remove when not requiring at generation water now in the straightforward procedure of water and manufacture cyclic acetal and contracting with high yield
Ketone.It is different from unless removed water during the water as by-product is formed, the expection that yield can be the lowest, this
Bright method can make all raw material react to manufacture reactant mixture in a reactor in the liquid phase, and it takes in the liquid phase
Go out and distill subsequently, thus manufacturing required cyclic acetal or ketal with high yield.
There is presently provided the continuity method for manufacturing cyclic acetal or ketal compound, comprising:
A. being supplied under all polyols of reactor and the mol ratio of all carbonyl compounds at least 3:1,
The carbonyl composition comprising aldehyde compound, ketonic compound or a combination thereof and the polyhydroxy compositions comprising polyol are supplied
To reactor；With
The most in the reactor, make carbonyl composition and polyol react in the presence of homogeneous acid catalyst with
Reactor generates the even in liquid phase reaction comprising cyclic compound, water, acid catalyst and unreacted polyol mixed
Compound；With
From reactant mixture, water is not separated, as liquid product stream from reaction when forming water the most in the reactive mixture
Device is continuously withdrawn described even in liquid phase reactant mixture；With
D. liquid reacting product stream is directly or indirectly supplied to distillation column with by cyclic compound and unreacted polyhydroxy
Compound separates and takes out overhead stream and bottoms product steam from distillation column, and wherein overhead stream comprises ring-type chemical combination
Thing, unreacted carbonyl compound and water and compared with bottoms product steam the molar concentration of cyclic compound high, and tower bottom product
Stream comprise unreacted polyol and acid catalyst and compared with overhead stream unreacted polyol
Molar concentration is high；
Wherein in overhead stream, selectivity to cyclic compound is at least 80%.
The cyclic acetal taken out in overhead stream or the yield of ketal compound can also be at least 80%.
In the method for the invention, it is also possible at least some of the most anti-by take out from distillation column in bottoms product steam
The polyol answered is recycled to reactor.Non-aqueous reaction by-product can also be taken out to produce richness from bottoms product steam
Polyhydroxy base flow and be rich in machine byproduct stream, hereafter can make at least some of polyol in rich polyhydroxy base flow and acid urge
Agent is recycled to reactor.
4. Accompanying drawing is sketched
Fig. 1 is to manufacture cyclic acetal or ketal compound in the reactor, then distill, separate and by a part of polyhydroxy
Compound is recycled to the process chart of reactor.
5. Detailed Description Of The Invention
There is presently provided the continuity method for manufacturing cyclic compound.Cyclic compound refers to the compound with ring structure,
Described ring structure has two oxygen atoms in the identical carbon atoms being singly bonded in this ring structure in this ring structure.This is ring-type
Compound can be cyclic acetal compounds or cyclic ketal compound.By being supplied to all many of reactor at least 3:1
Under the mol ratio of hydroxy compounds and all aldehydes or ketones compounds, by carbonyl compound and the polyhydroxy comprising polyol
Compositions is supplied to reactor, manufactures cyclic compound.Carbonyl compound refers to that aldehyde compound, ketonic compound (depend on wanting system
Make acetal or ketal) or both mixture.
It is supplied to the aldehydes or ketones compound that the carbonyl composition of reactor contains one or more types.Aldehyde compound contain to
Few aldehyde official's energy.Aldehyde and ketonic compound can be represented by Formulas I:
Wherein R1And R2Independently be hydrogen or C1-C50Alkyl, C2-C50Thiazolinyl, aryl-C1-C50Alkyl, aryl-C2-C50Alkene
Base-or C3-C12Cycloalkyl, and wherein R1And R2Optionally connect via one or more carbon atoms, and wherein R1And R2Alkyl,
Alkenyl, aryl and cycloalkyl be the most saturated or unsaturated and branched or non-branching or by 1,2 or 3 comprise-OH, halogen,
Dialkyl amido, C1-C6Alkyl, aldehyde, ketone, carboxylic acid, ester, ether, alkynyl, dialkyl amide, acid anhydride, carbonic ester, epoxide, lactone,
The group of lactams, phosphine, silicyl, thioether, mercaptan, aryl, phenol or a combination thereof replaces or unsubstituted；And wherein work as R1Or R2
One of when being hydrogen, this compound is aldehyde, and wherein works as R1And R2When being not hydrogen, this compound is ketone.
If it is required, this aldehyde compound can have at least one aldehyde functional group, wherein aldehyde carbon atom bonding is branched to (i)
Or non-branching C1-C9Alkyl or (ii) are optionally branched or non-branching C1-C9On the substituted aryl of alkyl or alcyl.
The example of aldehyde compound includes, but not limited to benzaldehyde, acetaldehyde, propionic aldehyde, butyraldehyde, isobutylaldehyde, valeral, 2-methyl
Butyraldehyde, 3-methylbutyraldehyd, valeraldehyde, isovaleral, hexanal, enanthaldehyde, 2-ethyl hexanal, octanal, aldehyde C-9, n-capric aldehyde, 2-methyl ten
One aldehyde, lauryl aldehyde, myristic aldehyde, spermaceti aldehyde, stearaldehyde, behenyl aldehyde, glutaraldehyde, acrylic aldehyde, crotonic aldehyde, oil aldehyde, sub-oil aldehyde, Asia
Fiber crops aldehyde, erucyl aldehyde, cinnamic aldehyde, 1,3-cyclohexanedicarboxaldehyde, 1,4-cyclohexanedicarboxaldehyde and combinations thereof.
The example of ketonic compound includes, but not limited to acetone, butanone (2-butanone), methyl propyl ketone (2 pentanone), first
Base nezukone (3-methyl-2-butanone), methyl iso-butyl ketone (MIBK) (4-methyl-2 pentanone), methyl-n-butyl ketone, 2-heptanone (methyl amyl
Ketone), methyln-hexyl ketone and 1-Phenylethanone. and combinations thereof.
It is supplied to the polyol that the polyhydroxy compositions of reactor contains one or more types.Polyol
There is at least two hydroxyl (-OH) sense.This polyol can contain ether or ester bond in Long carbon chain.
Be applicable to the polyol of the present invention include, but are not limited to ethylene glycol, 1,2-PD, 1,3-PD,
1,4-butanediol, 1,3 butylene glycol, 1,2-butanediol, 1,2-pentanediol, 2,4-PD, 2,2-dimethyl-1,3-propylene glycol,
Diethylene glycol and triethylene glycol, glycerol, trimethylolpropane, xylitol, arabitol, 1,2-or 1,3 ring pentanediols, 1,2-or 1,
3-cyclohexanediol and 2,3-norbornane glycol.
The cumulative amount of the polyol and carbonyl compound that are supplied to reactor is at least 3:1 or at least 4:1 or big
In 5:1 or at least 6:1 or at least 7:1 or at least 8:1 or at least 9:1 or at least 10:1 or at least 13:1 polyol/
Carbonyl compound (aldehydes or ketones compound) mol ratio.There is no the specific upper limit.Balance use be enough to improve required cyclic acetal or contracting
The selectivity of ketone and the needs of the excess of yield, the amount that limiting needs to separate the polyol with recirculation is economically to close
Meaning.It practice, the mol ratio of polyol and carbonyl compound need not more than 30:1, or no more than 20:1, even
It is not more than 15:1.
The mol ratio of polyol and carbonyl compound is determined by the total amount being supplied to reactor.If by polyhydroxy
The recirculation flow of compound is supplied to reaction zone, it should this gauge is entered this mol ratio.
Polyhydroxy compositions and carbonyl compound compositions as individually stream or can be supplied to reactor as merging stream.As
Fruit differences in viscosity between the two is sufficiently large, preferably by pre-with at least some of carbonyl compound at least some of polyhydroxy compositions
Mixed to improve yield and the contact point quantity improved between aldehydes or ketones official energy and hydroxyl-functional.As shown in fig. 1, polyhydroxy combination
Logistics 1 and carbonyl compound compositions stream 2 premixed before enter reactor via reactant feed flow 3 in mixed zone.Also
Recirculation flow 10 containing unreacted polyol and acid catalyst can be supplied to mixed zone with by all carbonylations
Compound is sufficiently mixed and dispersed or be dissolved in polyhydroxy compositions, if the viscosity of especially polyhydroxy compositions is obvious
Higher than carbonyl composition.
If polyhydroxy compositions and carbonyl composition is arbitrary or both viscosity is the highest so that cannot provide satisfactory
If mixing arbitrary or both be solid at ambient conditions, can preheat arbitrary or both.Polyol and carbonyl
Based compound should be liquid when entering reactor.
The polyol and the carbonyl compound that are supplied to reactor react in the presence of homogeneous acid catalyst.Acid catalyst
Example include Br nsted-Lowry acid.Available acid includes hydrochloric acid, sulphuric acid, phosphoric acid, Fluohydric acid., hydrobromic acid, hydroiodic acid, hydrogen
Perchloric acid (hydroperchloric acid), p-methyl benzenesulfonic acid and methanesulfonic acid, trifluoromethanesulfonic acid (triflic acid), trifluoro
Acetic acid and p-methyl benzenesulfonic acid.These acid can be liquid or aqueous solution and be formed homogeneous in liquid reaction medium.
Acid catalyst can individually be supplied to reactor or premix and combine logistics 1, carbonyl group to the polyhydroxy being supplied to reactor
In one or both of compound stream 2, recirculation flow 10 or reaction logistics 3.This reactor contains homogeneous reaction mixture, it is meant that acid
Catalyst forms homogeneous solution with other composition in the reactor, so that the content of this reactor is uniform liquid phase reactor
Mixture, is different from the reactor containing the solid catalyst being dispersed in liquid reaction mixture or stationary catalyst bed.
This reactor is to connect before carbonyl compound and polyol interreaction in the presence of a homogeneous catalyst
Receive carbonyl compound and the charging of polyol or the container of multiple charging.This reactor can also receive containing carbonyl or
The recirculation charging of polyol or homogeneous acid, it was once a part for reactant mixture in reactor but with regard to carbonyl
Or unreacted for polyol.Owing to this homogeneous catalyst is flowing, it will be recognized that reaction may be at distillation container
In or proceed in the downstream reservoir of distillation column, these containers are different from reactor.
The reactant mixture that this reactor is desirably in full liquid and reactor flows to drain position from feed entrance point.
In horizontal vessel, this can be according to charging/discharge structure level stream from left to right or from right to left.Vertical orientated
In container, this can be from head-to-foot or from bottom to top.In one embodiment, the reactant mixture in reactor the end of to
Overhead stream moves.By make feed entrance point be positioned at reactor bottom or its near and make effluent be positioned at reactor head, it is thus achieved that more
Good mixing.
Reactor can be contained in any suitable container.In one embodiment, this reactor is to have to be more than
1:1, or more than 2:1, or more than 3:1, or more than 4:1, or more than 5:1, or more than 6:1, or more than 7:1, or more than 8:1, or
More than 9:1, or it is more than pipe or the groove of the L/D ratio of 10:1.
This reactor can be with mechanical agitation.It practice, this reactor does not has mechanical agitation.It is, for example possible to use mechanical
The pipe of stirring, although if desired, the stirring that this pipe can induce to provide turbulent flow containing weir plate or baffle plate.
This reaction can under atmospheric pressure and the most well be carried out.Pressure in reactor can be to
Few 0.1 atm, or at least 0.5 atm, or at least 1 atm, or at least 1.05 atm, or at least 1.1 atm, or at least 1.5
Atm, or at least 2 atm, or at least 3 atm, or at least 4 atm.For most of purposes, pressure needs not exceed 10
Atm, or more than 5 atm, or more than 3 atm, or more than 2 atm.
In reactor, polyol reacts generation cyclic acetal or cyclic ketal with carbonyl compound or it mixes
Thing, water and by-product.For purposes of this specification, cyclic acetal is made up of the reaction of raw material aldehyde and raw material polyol
Required primary product.Primary product cyclic acetal is the ring-type of 1 mole starting material aldehyde compound and 1 mole starting material polyol
Product, discharges 1 mole of water.Manufacture the example of by-product in the reactant mixture of cyclic acetal be aldehyde-aldehyde reaction product,
Polyhydroxy-polyhydroxy product, cyclic acetal and other reactant any or with itself between secondary response product, ring
The internal rearrangement of shape acetal ring and reset other product any or a combination thereof produced by ring.Owing to using high molar excess
Polyol, there is also unreacted polyol in the reactive mixture.This reactant mixture also can contain
Unreacted aldehyde compound.
This is equally applicable to the manufacture of cyclic ketal.For purposes of this specification, cyclic ketal is many by raw ketone and raw material
The required primary product that the reaction of hydroxy compounds is made.Primary product cyclic ketal is 1 mole starting material ketonic compound and 1 mole
The oligomer product of raw material polyol, discharges 1 mole of water.Manufacture the by-product in the reactant mixture of cyclic ketal
Example be ketone-one product, polyhydroxy-polyhydroxy product, cyclic ketal and other reactant any or with its
Secondary response product between body, the internal rearrangement of cyclic ketal ring and reset other product any or its produced by ring
Combination.Owing to using the polyol of high molar excess, there is also unreacted polyhydroxy chemical combination in the reactive mixture
Thing.This reactant mixture also can contain unreacted ketonic compound.
By by the molal quantity of the product Compound made divided by the reactant fed with minimum mole molal quantity again
It is multiplied by 100, measures the yield of product Compound (rather than by-product or water), no matter want to measure cyclic compound, acetal chemical combination
Thing or the yield of ketal compound.Such as, by the molal quantity of cyclic compound that will make divided by the corresponding aldehyde fed and/
Or the molal quantity of ketonic compound is multiplied by 100 again, measure the yield of cyclic compound.By the cyclic acetal compounds that will make
Molal quantity is multiplied by 100 again divided by the molal quantity of the aldehyde compound fed, and measures the yield of cyclic acetal compounds.By making
The molal quantity of cyclic ketal compound be multiplied by 100 again divided by the molal quantity of ketonic compound fed, measure cyclic ketal chemical combination
The yield of thing.
By the molal quantity of cyclic compound that will make divided by each of which converted aldehydes or ketones compound mole
Number is multiplied by 100 again, measures the selectivity of cyclic compound.By the molal quantity of cyclic acetal compounds that will make divided by conversion
The molal quantity of aldehyde compound be multiplied by 100 again, measure the selectivity to cyclic acetal.By the cyclic ketal compound that will make
Molal quantity be multiplied by 100 again divided by the molal quantity of ketonic compound converted, measure the selectivity to cyclic ketal.
By the molal quantity of the cyclic compound of conversion is taken advantage of divided by the molal quantity of the respective aldehydes or ketones compound fed again
With 100, measure the conversion ratio to cyclic compound.By will convert cyclic acetal compounds molal quantity divided by feed aldehyde
The molal quantity of compound is multiplied by 100 again, measures the conversion ratio to cyclic acetal.By rubbing the cyclic ketal compound of conversion
That number is multiplied by 100 again divided by the molal quantity of the ketonic compound fed, and measures the conversion ratio to cyclic ketal.
In the method for the invention, it is not necessary in the reactive mixture formed water time from reactant mixture separating by-products water
It is achieved with the high yield of cyclic compound.Even if this reaction is that exist can hydrolysis of acetals or ketal product reduce yield
The balancing response of water, the polyol of high molar excess and aldehyde compound reaction in presence of an acid also make cyclic acetal
Selectivity and yield keep height.This have need not in the reactor when water is formed by distillation or alternate manner except water to obtain
The advantage obtaining high yield.Additionally, reacting processing window broadens and not by the boiling point model of reactant and product and by-product
Enclose restriction.
The oligomer product formed in the reactive mixture contain ethylidene ether structure part or ketal structure part or both.
Two oxygen that the cyclic compound made in the method for the present invention has in the identical carbon atoms being singly bonded in this ring structure are former
Son.Suitably cyclic acetal and ketal moieties includes 1,3-dioxolane structure part and 1,3-dioxane structure portion
Point, although being also contemplated for 1,3 positions have the more macrocyclic compound of oxygen atom.
The ring-type chemical combination including cyclic acetal structure division or cyclic ketal structure part made in the method for the present invention
Thing can be represented by formula II:
Wherein R1、R2、R3And R4Independently be H；Branched or non-branching C1-C50Alkyl, C2-C50Thiazolinyl, aryl-C1-C50Alkane
Base, aryl-C2-C50Thiazolinyl-, C3-C12Cycloalkyl or C3-C50Carboxylate；And wherein R1And R2The most former via one or more carbon
Son bonding mutually, and wherein R1、R2、R3And R4Optionally containing 1,2 or 3 oxygen atoms in alkyl or alkenyl, and wherein R1、R2、
R3And R4Alkyl, thiazolinyl, aryl and cycloalkyl optionally by 1,2 or 3 independently selected from-OH, halogen, dialkyl amido, aldehyde,
Ketone, carboxylic acid, ester, ether, alkynyl, dialkyl amide, acid anhydride, carbonic ester, epoxide, lactone, lactams, phosphine, silicyl, sulfur
The group of ether, mercaptan and phenol replaces；
Wherein R3And R4Any one or both optionally independently be hydroxyl, halogen, dialkyl amido, amine, aldehyde, ketone, carboxylic
Acid, ester, ether, alkynyl, dialkyl amide, acid anhydride, carbonic ester, epoxide, lactone, lactams, phosphine, silicyl, thioether, mercaptan
Or phenol；
Wherein R5It is each to there is 1 to 20 carbon atom and optionally contain 1,2 or 3 oxygen atoms also in alkyl or alkenyl
Optionally by-OH, halogen, dialkyl amido, aldehyde, ketone, carboxylic acid, ester, ether, alkynyl, aryl, dialkyl amide, acid anhydride, carbonic ester, ring
Oxide, lactone, lactams, phosphine, silicyl, thioether, mercaptan and phenol is substituted branched or non-branching divalent alkyl or bivalence
Thiazolinyl；And
Wherein nIt it is the integer selected from 0 or 1.
R1、R2、R3And R4H or branched or non-branching C can be independently be1-C6Alkyl.Or R1、R2、R3And R4Can be independent
Ground is H or branched or non-branching C1-C4Alkyl.R1Can be branched or non-branching C1-C6Alkyl, simultaneously R2It is that hydrogen atom is to provide
Cyclic acetal.
R5Can be that there is 1 to 6, or 1 to 4, or 1 to 3, or the branched or non-branching divalent alkyl of 1 to 2 carbon atom.
The cyclic acetal being particularly useful for the commercial materials that the present invention can use with offer includes DOX, wherein R1
Being alkyl, it provides " E-series " type solvent.The 1,3-dioxolanes that R1 is alkyl and R3 is methyl can provide " P-system equally
Row " type solvent.
The example of cyclic acetal include 2-propyl group-1,3-dioxolanes, 2-propyl group-1,3-dioxane, 2-ethyl-
1,3-dioxolanes, 2-ethyl-1,3-dioxane, 2-methyl-1,3-dioxy penta ring, 2-methyl-1,3-dioxy heterocyclic
Hexane, 2-propyl group-4-methyl-1,3-dioxy heterocyclic hexane, 5,5-dimethyl-2-propyl group-1,3-dioxane, 5,5-bis-
Methyl-2-ethyl-1,3-dioxane, 2-ethyl-1,3-Dioxepane (dioxepane), 2-ethyl-1,3,6-
Trioxacane (trioxocane), 4-methanol-2-propyl group-1,3-dioxolanes or 4-methanol-2-propyl group-1,3-dioxa
Hexamethylene, 4-methanol-2-propyl group-1,3-dioxolanes and 2-propyl group-1,3-dioxane-4-alcohol.
The example of cyclic ketal includes 2,2-dimethyl-1,3-dioxolanes, 2,2-dimethyl-1,3-dioxa hexamethylene
Alkane, 2,2,4-trimethyl-1,3-dioxolanes, 2,2-dimethyl-1,3-Dioxepane, 4-methanol-2,2-dimethyl-1,
3-dioxane, 2,2-dimethyl-1,3-dioxan-4-ol, 2,2-dimethyl-1,3-6-trioxacane, 2-are different
Propyl group-2-methyl-1,3-dioxy penta ring, 2-isopropyl-2-methyl-1,3-dioxy heterocyclic hexane, 2-isopropyl-2,4-diformazan
Base-1,3-dioxolanes, 2-isopropyl-2-methyl-1,3-dioxy heterocyclic heptane, 4-methanol-2-isopropyl-2-methyl isophthalic acid, 3-
Dioxane, 2-isopropyl-2-methyl isophthalic acid, 3-dioxan-4-ol, 2-isopropyl-2-methyl isophthalic acid, 3-6-trioxa ring is pungent
Alkane, 2-methyl-2-amyl group-1,3-dioxolanes, 2-methyl-2-amyl group-1,3-dioxane, 2,4-dimethyl-2-penta
Base-1,3-dioxolanes, 2-methyl-2-amyl group-1,3-Dioxepane, 2-methyl-2-amyl group-4-methanol-1,3-dioxy
Penta ring, 2-methyl-2-amyl group-1,3-dioxan-4-ol, 2-methyl-2-amyl group-1,3-6-trioxacane.
Take out from reactor before reactant mixture not reaction mixture to separate water from reactant mixture.
This reactor is full liquid, and wherein the liquid in reactor is sufficiently mixed or with plug flow feeding.Reaction temperature is not by spy
Do not limit.Reaction condition in reactor desirably makes reactant mixture keep liquid and not be set as that exceeding this mixture exists
Boiling point under reaction condition.Suitably reaction temperature is at least-15 DEG C, or at least 0 DEG C, or at least 15 DEG C, or at least 25 DEG C, or
At least 30 DEG C, or at least 40 DEG C, and desirably less than 110 DEG C, most 90 DEG C, or most 70 DEG C, or most 50 DEG C.
Reactant mixture takes out from reactor as product liquid Flow Line 4 as shown in fig. 1.If at liquid form
Product stream in there is water, cyclic compound and polyol and under reactor condition, do not stand height in the reactor
In the temperature of the boiling point of this mixture, this product stream is considered liquid product stream.
The liquid product stream taken out from reactor is also unique compositions.There is presently provided and comprise water, polyhydroxy chemical combination
Thing and the fluid composition of cyclic compound, the most following molar percentage, based in said composition all liq mole
Number:
A. water: at least 2 moles of %, or at least 3 moles of %, or at least 6 moles of %, or at least 8 moles of %, or at least 10 rub
You are %, and most 35 moles of %, or most 25 moles of %, or most 20 moles of %, or most 15 moles of %；
B. polyol: at least 50 moles of %, or at least 60 moles of %, or at least 65 moles of %, or at least 70 rub
You are %, and most 95 moles of %, or most 90 moles of %, or most 85 moles of %；
C. cyclic compound: at least 2 moles of %, or at least 3 moles of %, or at least 5 moles of %, or at least 7 moles of %, and
Many 35 moles of %, or most 25 moles of %, or most 20 moles of %, or most 15 moles of %；
The most described catalyst: at least 0.01 mole of %, or at least 0.1 mole of %, or at least 0.2 mole of %, or at least 0.25
Mole %, and 3 moles of % or most of 4 moles of % or most of most 5 moles of % or most, 1 mole of % or most 0.75 of 2 moles of % or most
Mole %；
Wherein this fluid composition optionally contains carbonyl compound, and it is if it does, be less than cyclic compound molal quantity
20%, and wherein if it does, except a), b), c) and all liq composition tired of carbonyl compound beyond the region of objective existence in this fluid composition
Metering is less than 10 moles of %, and this cyclic compound comprises cyclic acetal, cyclic ketal or a combination thereof.
This fluid composition optionally contains carbonyl compound (i.e. aldehyde and/or ketonic compound), and it is if it does, be less than ring
The cumulative amount of the 15% of shape compound molal quantity, or less than 12%, and wherein other liquid component any in this fluid composition
Amount less than 8 moles of %, or less than 6 moles of %.
Cyclic compound in this liquid product stream can be cyclic acetal or cyclic ketal.By product liquid Flow Line 4
Directly or indirectly it is sent to distillation column to separate as the cyclic compound of one or more overhead stream and water and unreacted
Carbonyl compound and as the unreacted polyol of one or more bottoms product steam and acid catalyst.This tower top produces
Logistics can be the single overhead stream as shown in the circuit 5 of Fig. 1 or multiple overhead stream.The tower top leaving distillation column produces
Logistics is desirably steam stream.At least some of condensable compound in these steam streams desirably condenses for use as backflow
And/or separate available cyclic acetal product, purify liquid ring acetal product thereafter through Conventional concentration and/or isolation technics
Concentration.
As shown in fig. 1, distillation column has overhead product Flow Line 5, and it is desirably steam also when leaving distillation column
And it is possible if desired to condensation.With bottoms product steam present in cyclic compound weight concentration compared with, leave the tower of this tower
The weight concentration of top product stream cyclic compound is high, or in other words, in overhead stream, the amount of cyclic compound is more than as tower
The amount of the cyclic compound that bottom product stream takes out from distillation column.This is preferably applied to water, i.e. there is water in overhead stream
And the concentration in overhead stream is more than the concentration in bottoms product steam.Enrichment refers to the concentration (based on mole %) in a stream
Higher than the concentration of same composition in contrast stream, and to impinging upon all compounds (condensables) of condensation under 0 DEG C or higher temperature
Measure this concentration.Similarly, compared with the concentration of carbonyl compound unreacted with bottoms product steam, overhead stream unreacted
The molar concentration of carbonyl compound high.
Although overhead stream may contain unreacted polyol, but with its existence in bottoms product steam
Amount (molar concentration) is compared, the amount of overhead stream shortcoming (molar concentration is relatively low) this composition.Therefore, with in overhead stream
Existence number compare, bottoms product steam is rich in unreacted polyol quantity.Bottoms product steam leaves steaming as liquid stream
Evaporate tower.Bottoms product steam also can contain non-aqueous by-product.If there is by-product, the amount in bottoms product steam more preferably greater than
Amount in overhead stream.
In distillation column, the quantity of theoretical stage (stage) or plate can be about 5 to about 100, or about 10-30 plate.
Within the condenser overhead stream can be imposed condensation.Collecting condensation and is appointed in memorizer or return tank
Gated any conventional tool, as decanter separates.Extract the top rich organic phase of condensate in memorizer and as product
Reclaim, and can be processed further and purify with isolated and purified cyclic compound stream.The lower section phase rich water of this memorizer, from storage
Device takes out and is sent to water processing establishment or is processed further.Replace condenser, overhead stream can be fed after-fractionating
Tower is to separate water with required cyclic compound with unreacted carbonyl compound.
Table 1 below shows mole % scope of each composition taken out from distillation column arranges and in overhead stream after decantation
(concentration range) (includes the combination of aqueous phase and organic facies), wherein said mole of % weight based on all the components in tower top stream:
Table 1
| Composition | Mole % | Mole % | Mole % |
| Water | 30-50% | 44-50% | 47-49% |
| Unreacted carbonyl compound | 0.1-20% | 2-8% | 4-6% |
| By-product | 0-10% | 0-5.0% | 1.0-2.0% |
| Cyclic compound (acetal, ketal or combination) | 30-50% | 40-50% | 43.0-44.0% |
| Polyol | 0-20% | 0-4.0% | 0.5-1.0% |
Mole % scope of each composition that the value in upper table 1 is also applied in overhead stream, wherein said molar percentage
Cumulative number of moles based on all fresh feeds entering this process.
The product stream leaving reactor can be optionally through one or more processing steps before entering distillation column.
It is possible if desired to bottoms product steam 6 is imposed further processing step.Such as, present in bottoms product steam
Unreacted polyol and liquid acid catalyst can be separated from bottoms product steam by any conventional isolation techniques.
A kind of such Advantageous techniques is bottoms product steam to feed subsider and by unreacted polyol and by-product phase
Separate.By-product advantageously acts as top layer and is separated and can decant and as byproduct stream 7 and polyhydroxy/acid catalyst bottom
Separate, simultaneously position removing polyhydroxy/acid catalyst bottom below byproduct layer as shown in stream 9 and 10.Or, can
So that bottoms product steam is imposed extraction and separation technology, thus the hydrocarbon extractant serving as the solvent of relatively hydrophobic by-product is produced at the bottom of tower
Logistics mixes to help separating by-products stream.Such as, organic solvent can be used for extracting by-product and introducing extraction via stream 8
District.Suitably solvent includes having 4 carbon to more than 20 carbon, saturated and undersaturated, liquid with and without circulus
Body hydrocarbon, aliphatic series and cyclic ether, ester, fatty acid, halogenated hydrocarbons, fatty nitrile and aliphatic series and aromatic amine.The instantiation bag of organic solvent
Include heptane, octane and nonane.
From bottoms product steam, generally separate polyol and acid catalyst, can will be recirculated back at least partially
Reactor.As shown in fig. 1, stream 10 separates and leaves the part of blender/settler from bottoms product steam
Or all polyols and acid catalyst send the mixed zone to reactor feed back to.If there is mixed zone with by carbonyl
Based compound is dispersed in polyhydroxy compositions, preferably recirculation flow 10 is supplied to mixed zone.Divide from bottoms product steam
From a part of polyol and acid catalyst can via stream 9 remove (purge) and be processed further with purify and again
Utilize this removing stream.
The method of the present invention can produce at least the 80% of the aldehyde compound amount being supplied to reactor, or at least 84%, or at least
85%, or at least 86%, or at least 88%, or at least 89% and most 100%, or most 98%, or most 95%, or the ring of most 90%
Shape compound yield.The yield of cyclic compound in the overhead stream taken out can be conveniently measured by from distillation column come
Measure yield.
Wish to convert at least 80%, or at least 84%, or at least 84%, or at least 86%, or at least 88% and most 100%, or
The aldehydes or ketones compound of most 98%, or most 95%, or most 93%.
Selectivity to cyclic compound can be at least 90%, or at least 91%, or at least 92%, or at least 93%, or extremely
Few 94%, or at least 95%, or at least 96%, or at least 97%, or at least 98% and most 100%, or most 99.5%, or at most
99%。
The method of the present invention can be run with intermittent mode, semi-continuous mode or continuous mode.In continuous mode and
In steady-state operation, the method for the present invention has annual at least 70 tonnes of cyclic compounds, or at least 85 of producing, or at least 90, or
The productivity of at least 110 public tons/year.
Cyclic compound in the cyclic compound stream separated can convert to provide corresponding ether alcohol solvent by hydrogenolysis.Example
As, 2-propyl group-DOX, 2-propyl group-1,3-dioxane, 2-ethyl-DOX, 2-ethyl-1,
3-dioxane, 2-methyl-1,3-dioxy penta ring, 2-methyl-1,3-dioxy heterocyclic hexane, 5,5-dimethyl-2-propyl group-
1,3-dioxane, 2-ethyl-1,3-Dioxepane, 2-ethyl-1,3,6-trioxa hexamethylene octane, 4-methanol-
2-propyl group-1,3-dioxolanes or 2-propyl group-1,3-dioxane-4-alcohol fit through hydrogenolysis and manufacture the molten of each of which
Agent ethylene glycol monobutyl ether, 3-butoxy-1-propanol, ethylene glycol monopropyl ether, 3-propoxyl group-1-propanol, ethylene glycol list ethyl
Ether, 3-ethyoxyl-1-propanol, 3-butoxy-2,2-dimethyl-1-propanol, 4-propoxyl group-n-butyl alcohol and diethylene glycol mono butyl base
Ether, 3-butoxy-1,2-propylene glycol and 2-butoxy-1,3-propylene glycol.
Embodiment
Use following devices.Use jacketed glass container as reactor.Up-flow orientation is used to make it keep full liquid.
Also use distillation column.Distillation column has two sections, is respectively equipped with 0.24 " Pro-Pak distillation random packing 1 " vacuum jacket glass
Glass tower.Epimere has 15 " filler, hypomere has 30 " filler.Bottom reboiler is attached to 1 liter of deep fat folder bottom tower hypomere
Set glass container.The top of epimere be connected to band be magnetic rocking arm controller and jacketed glass condenser glass jacket backflow separate
Device.Subsidiary discharging hose is connected to ice trap (ice trap), pressure controller and vacuum pump.Teflon pipe is used to connect equipment.
It is connected to positive-displacement pump by pipeline bottom tower reboiler.
Pipeline from this pump discharge is connected to comprise the Disengagement zone of blender and settler.Glass feed container contains
Solvent.This solvent feed container is connected to positive-displacement pump.Pipeline from this pump and the pipeline from column bottoms pump are connected to one
Rise.This merging stream is connected to blender.This blender is the 30 milliliters of glass keeping full liquid containing agitator of magnetic drive
Container.Product stream from this blender is connected to 120 milliliters of jacketed glass containers, and it is settler.This container has two
Individual outlet, one at top, one in bottom.In running so that it is keep full liquid.Its jacket temperature set point keeps
At 90 DEG C.Top exit is connected to remove another positive-displacement pump of the material rich in solvent and by-product.Outlet at bottom passes through
Pipeline is connected to feed pump described below.
Use and accommodate aldehyde charging and the glass feed container of polyhydric alcohol charging respectively.It is connected to positive discharge capacity each via pipeline
Pump.Pipeline from the two feed pump and the pipeline from blender/settler link together.Merge stream to be connected to containing magnetic
Drive 30 milliliters of full liquid glass containers of agitator.This mixed flow is connected to reactor bottom, to complete fluid loop.Use
Process control system is monitored temperature and flow rate pump and uses tower temperature set-point to control distillation column reflux splitter.In each embodiment
In, use hutanal as carbonyl compound using the feed rate of 1 ml/min, use with the feed rate of 1 ml/min
Ethylene glycol is as polyol, and the feed rate of unconverted recycled materials is 8 ml/min.It is initially charged with liquid
Acid catalyst rather than in experimentation add.
Embodiment 1. phosphoric acid, 40 DEG C, octane solvent
1.8 grams of phosphoric acid are added in 400 grams of ethylene glycol and this solution is loaded bottom distillation column.By reactor jacket oil
Bath temperature is set as 40 DEG C.Will act as the octane of blender/settler solvent continuously, interval adds in blender, and from heavy
Fall device removes the octane stream rich in byproduct of reaction.The method runs 25 hours continuously.2-propyl group-1,3-dioxolanes total
Conversion ratio, selectivity and yield are high: be respectively 91.7%, 98.5% and 90.3%.
Embodiment 2. phosphoric acid, 22 DEG C, octane solvent
Method described in embodiment 1 continues to run with, but reactor jacket oil bath temperature is set as room temperature 22 DEG C.The party
Sole catalyst in method is to stay in embodiment 1.The method runs 24 hours continuously.2-propyl group-1,3-dioxolanes
Total conversion, selectivity and yield are high: be respectively 86.8%, 99.3% and 86.2%.
Embodiment 3. phosphoric acid, 40 DEG C, heptane solvent
Method described in embodiment 2 continues to run with, but reactor jacket oil bath temperature is set as 40 DEG C.In the method
Sole catalyst be that embodiment 2 stays.Replace octane, use heptane as blender/settler solvent.The method is even
Reforwarding row 53 hours.Owing to re-using the catalyst from the first two embodiment, accumulative catalyst run is 102 hours.
Conversion data does not show reduction, shows that catalyst activity does not lose.The total conversion of 2-propyl group-1,3-dioxolanes,
Selectivity and yield are high: be respectively 91.0%, 99.6% and 90.6%.
Claims (18)
1. the method manufacturing cyclic compound compositions, comprising:
A. all polyols of reactor that are supplied at least 3:1 will wrap under the mol ratio of all carbonyl compounds
Carbonyl composition and the polyhydroxy compositions comprising polyol of aldehyde-containing compounds, ketonic compound or a combination thereof are supplied to instead
Answer device；With
The most in the reactor, described carbonyl composition and described polyol is made to react in the presence of homogeneous acid catalyst
Anti-to generate the even in liquid phase comprising cyclic compound, water, acid catalyst and unreacted polyol in the reactor
Answer mixture；With
From reactant mixture, water is not separated, as liquid product stream from reaction when c. forming water in described reactant mixture
Device is continuously withdrawn described even in liquid phase reactant mixture；With
D. described liquid reacting product stream is directly or indirectly supplied to distillation column with by cyclic compound and unreacted polyhydroxy
Compound separates and takes out overhead stream and bottoms product steam from distillation column, and wherein overhead stream comprises ring-type chemical combination
Thing, unreacted carbonyl compound and water and compared with bottoms product steam the molar concentration of cyclic compound high, and tower bottom product
Stream comprise unreacted polyol and acid catalyst and compared with overhead stream unreacted polyol
Molar concentration is high；
In wherein said overhead stream, the selectivity to cyclic compound is at least 80%.
2. the process of claim 1 wherein and at least some of unreacted polyol is recirculated back to described reactor.
3. the process of claim 1 wherein that described bottoms product steam comprises byproduct of reaction further, and wherein by described reaction
By-product separates with unreacted polyol to produce rich polyhydroxy base flow and rich byproduct stream.
4. the process of claim 1 wherein the carbonyl compound shown in the contained I of described carbonyl composition:
Wherein R1And R2Independently be hydrogen or C1-C50Alkyl, C2-C50Thiazolinyl, aryl-C1-C50Alkyl, aryl-C2-C50Thiazolinyl-or
C3-C12Cycloalkyl, and wherein R1And R2Optionally connect via one or more carbon atoms, and wherein R1And R2Alkyl and thiazolinyl
It is branched or non-branching, and wherein R1And R2Alkyl, thiazolinyl, aryl and cycloalkyl by 1,2 or 3 comprise-OH, halogen, two
Alkyl amino, C1-C6Alkyl, aldehyde, ketone, carboxylic acid, ester, ether, alkynyl, dialkyl amide, acid anhydride, carbonic ester, epoxide, lactone, interior
The group of amide, phosphine, silicyl, thioether, mercaptan, aryl, phenol or a combination thereof replaces or unsubstituted.
5. the method for claim 4, wherein said carbonyl compound comprises acetaldehyde, propionic aldehyde, butyraldehyde, isobutylaldehyde, valeral, 2-methyl
Butyraldehyde, 3-methylbutyraldehyd, hexanal, enanthaldehyde, benzaldehyde, 2-ethyl hexanal, octanal, aldehyde C-9,1,3-cyclohexanedicarboxaldehyde, 1,4-ring
Hexane dicarbaldehyde or a combination thereof, and described polyol comprises ethylene glycol, 1,2-PD, 1,3-PD, Isosorbide-5-Nitrae-fourth
Glycol, 1,3 butylene glycol, 1,2-butanediol, 1,2-pentanediol, 2,4-PD, 2,2-dimethyl-1,3-propylene glycol, diethyl two
Alcohol and triethylene glycol, glycerol, trimethylolpropane, xylitol, arabitol, 1,2-or 1,3 ring pentanediols, 1,2-or 1,3-hexamethylene
Glycol, 2,3-norbornane glycol or a combination thereof.
6. the process of claim 1 wherein that described mol ratio is at least 5:1.
7. the process of claim 1 wherein that described carbonyl compound comprises Isosorbide-5-Nitrae-cyclohexanedicarboxaldehyde.
8. the process of claim 1 wherein that described reactor contains homogeneous acid catalyst, i.e. Bronsted-Lowry acid catalysis
Agent.
9. the method for claim 8, wherein said reactor is full liquid.
10. the method for claim 9, wherein said reactant mixture flows up in vertical orientated reactor.
The method of 11. claim 10, wherein said reactor is pipeline.
12. the process of claim 1 wherein that described cyclic compound contains the structure division shown in Formula II:
Wherein R1、R2、R3And R4Independently be H；Branched or non-branching C1-C50Alkyl, C2-C50Thiazolinyl, aryl-C1-C50Alkyl, virtue
Base-C2-C50Thiazolinyl-, C3-C12Cycloalkyl or C3-C50Carboxylate；Wherein R1And R2The most mutual via one or more carbon atoms
Bonding, and wherein R1、R2、R3And R4Optionally containing 1,2 or 3 oxygen atoms optionally only by 1,2 or 3 in alkyl or alkenyl
On the spot selected from-OH, halogen, dialkyl amido, aldehyde, ketone, carboxylic acid, ester, ether, alkynyl, dialkyl amide, acid anhydride, carbonic ester, epoxidation
The group of thing, lactone, lactams, phosphine, silicyl, thioether, mercaptan and phenol replaces；
Wherein R5It is each to there is 1 to 20 carbon atom and optionally contain 1,2 or 3 oxygen atoms the most optionally in alkyl or alkenyl
By-OH, halogen, dialkyl amido, aldehyde, ketone, carboxylic acid, ester, ether, alkynyl, aryl, dialkyl amide, acid anhydride, carbonic ester, epoxidation
Thing, lactone, lactams, phosphine, silicyl, thioether, mercaptan and phenol is substituted branched or non-branching divalent alkyl or bivalence thiazolinyl；
And
Wherein nIt it is the integer selected from 0 or 1.
The method of 13. claim 12, wherein said cyclic compound comprises 2-propyl group-DOX, 2-propyl group-1,3-
Dioxane, 2-ethyl-1,3-dioxolanes, 2-ethyl-1,3-dioxane, 2-methyl-1,3-dioxy penta ring,
2-methyl-1,3-dioxy heterocyclic hexane, 2-propyl group-4-methyl-1,3-dioxy heterocyclic hexane, 5,5-dimethyl-2-propyl group-1,3-
Dioxane, 5,5-dimethyl-2-ethyl-1,3-dioxane, 2-ethyl-1,3-Dioxepane, 2-second
Base-1,3,6-trioxa hexamethylene octane, 4-methanol-2-propyl group-1,3-dioxolanes or 4-methanol-2-propyl group-1,3-dioxa
Hexamethylene or a combination thereof.
14. the process of claim 1 wherein described liquid acid comprise hydrochloric acid, sulphuric acid, phosphoric acid, Fluohydric acid., hydrobromic acid, hydroiodic acid,
Hydrogen perchloric acid, p-methyl benzenesulfonic acid, methanesulfonic acid, trifluoromethanesulfonic acid, trifluoroacetic acid or a combination thereof.
15. the process of claim 1 wherein that the reaction condition in described reactor makes reactant mixture keep liquid and not set
It is set to the boiling point exceeding described reactant mixture under reactor service condition.
16. the process of claim 1 wherein that the temperature in reactor is 15 DEG C to 70 DEG C.
The method of 17. any one of claim 1-16, wherein said method be the yield of continuous print and cyclic compound be at least
80%。
18. the process of claim 1 wherein that the yield of cyclic compound is at least 85% in overhead stream.
Applications Claiming Priority (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US13/168374 | 2011-06-24 | ||
| US13/168,374 | 2011-06-24 | ||
| US13/168,374 US8969598B2 (en) | 2011-06-24 | 2011-06-24 | Production of cyclic acetals or ketals using liquid-phase acid catalysts |
| PCT/US2012/042458 WO2012177485A1 (en) | 2011-06-24 | 2012-06-14 | Production of cyclic acetals or ketals using liquid-phase acid catalysts |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103619830A CN103619830A (en) | 2014-03-05 |
| CN103619830B true CN103619830B (en) | 2016-11-16 |
Family
ID=46331732
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201280030098.4A Active CN103619830B (en) | 2011-06-24 | 2012-06-14 | Liquid phase acid catalyst is used to manufacture cyclic acetal or ketal |
Country Status (3)
| Country | Link |
|---|---|
| US (2) | US8969598B2 (en) |
| CN (1) | CN103619830B (en) |
| WO (1) | WO2012177485A1 (en) |
Families Citing this family (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8829207B2 (en) | 2011-06-24 | 2014-09-09 | Eastman Chemical Company | Production of cyclic acetals by reactive distillation |
| US8969598B2 (en) | 2011-06-24 | 2015-03-03 | Eastman Chemical Company | Production of cyclic acetals or ketals using liquid-phase acid catalysts |
| US8829206B2 (en) | 2011-06-24 | 2014-09-09 | Eastman Chemical Company | Production of cyclic acetals or ketals using solid acid catalysts |
| US8785697B2 (en) | 2011-06-24 | 2014-07-22 | Eastman Chemical Company | Nickel modified catalyst for the production of hydroxy ether hydrocarbons by vapor phase hydrogenolysis of cyclic acetals and ketals |
| CN104311559A (en) * | 2014-09-12 | 2015-01-28 | 中山大学 | Synthetic method of optically pure chiral annular N, N-acetal |
| CN105712841B (en) * | 2014-12-05 | 2017-10-27 | 中国石油化工股份有限公司 | A kind of method of the propane diols of the separation and Extraction from zymotic fluid 1,3 |
| CN104945367A (en) * | 2015-06-04 | 2015-09-30 | 聂超 | Benzaldehyde propylene glycolacetal and preparation method thereof |
| CN106632229B (en) * | 2015-11-04 | 2019-04-05 | 中国科学院大连化学物理研究所 | A kind of preparation method of cyclic acetal |
| CN105693686B (en) * | 2016-03-10 | 2020-11-17 | 天津大学 | Reactive distillation method and device for 4EMD production |
| EP3929175A1 (en) | 2017-06-16 | 2021-12-29 | Rhodia Operations | Process for the catalytic decarboxylative cross-ketonization of aryl and aliphatic carboxylic acids |
| WO2019092495A1 (en) | 2017-11-09 | 2019-05-16 | Braskem S.A. | Process for the recovery of ketones and glycols from fermentation |
| KR20210013132A (en) * | 2018-05-18 | 2021-02-03 | 바스프 에스이 | Method for producing dioxolane |
| KR20210013131A (en) * | 2018-05-18 | 2021-02-03 | 바스프 에스이 | Method for producing dioxolane |
| CN108863734B (en) * | 2018-07-11 | 2021-02-19 | 华南理工大学 | Benzaldehyde di-bornyl acetal derivative and preparation method and application thereof |
| US10988491B2 (en) | 2018-08-17 | 2021-04-27 | Massachusetts Institute Of Technology | Degradable polymers of a cyclic silyl ether and uses thereof |
| EP4058501A1 (en) | 2019-11-15 | 2022-09-21 | Massachusetts Institute of Technology | Functional oligomers and functional polymers including hydroxylated polymers and conjugates thereof and uses thereof |
| US12030980B2 (en) | 2021-02-01 | 2024-07-09 | Massachusetts Institute Of Technology | Reprocessable compositions |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5446210A (en) * | 1991-07-20 | 1995-08-29 | Henkel Kommanditgesellschaft Auf Aktien | Process for the production of polyol ethers |
| US5917059A (en) * | 1996-11-15 | 1999-06-29 | Basf Aktiengesellschaft | Preparation of cyclic acetals or ketals |
Family Cites Families (109)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE419223C (en) | 1924-02-02 | 1925-09-22 | Hoechst Ag | Process for the production of solutions of organic bodies |
| US2425042A (en) | 1943-12-01 | 1947-08-05 | Carbide & Carbon Chem Corp | Glycol diethers |
| US2429878A (en) | 1946-05-17 | 1947-10-28 | Du Pont | Synthesis of glycol ethers |
| US2486024A (en) | 1947-08-19 | 1949-10-25 | Shell Dev | Preparation of polyalkylene glycols |
| DE1185604B (en) | 1962-02-03 | 1965-01-21 | Bayer Ag | Process for the production of vinyl acetate |
| BE653656A (en) | 1963-09-30 | 1965-03-29 | ||
| GB1046608A (en) | 1965-09-14 | 1966-10-26 | Shell Int Research | Cyclic acetals and ketals and their preparation |
| US4024159A (en) | 1974-08-07 | 1977-05-17 | E. I. Du Pont De Nemours And Company | Process for the production of liquid acetals |
| US4038175A (en) | 1974-09-23 | 1977-07-26 | Union Carbide Corporation | Supported metal catalyst, methods of making same, and processing using same |
| US4062898A (en) | 1975-10-06 | 1977-12-13 | Ethyl Corporation | Conversion of acetals |
| US4071568A (en) | 1975-12-12 | 1978-01-31 | Mitsubishi Chemical Industries Limited | Process for producing glycol monoether |
| JPS6044290B2 (en) | 1975-12-18 | 1985-10-02 | 三菱化学株式会社 | Method for producing glycol monoether |
| US4088700A (en) | 1976-09-27 | 1978-05-09 | Texaco Development Corporation | Process for the hydrogenolysis of dioxolanes |
| DE2716690A1 (en) | 1977-04-15 | 1978-10-19 | Hoechst Ag | PROCESS FOR THE PRODUCTION OF ETHYLENE GLYCOL DIMETHYL ETHER (DIMETHYL GLYCOL) |
| EP0019999B1 (en) | 1979-05-02 | 1983-09-07 | Imperial Chemical Industries Plc | Acetals and their preparation |
| JPS56166186A (en) | 1980-05-27 | 1981-12-21 | Mitsubishi Chem Ind Ltd | Production of cyclic acetal |
| US4308403A (en) | 1980-09-12 | 1981-12-29 | Texaco Inc. | Process for preparing glycol ethers |
| US4317943A (en) | 1980-09-12 | 1982-03-02 | Texaco Inc. | Process for preparing glycol ethers |
| US4479017A (en) | 1981-06-29 | 1984-10-23 | Mitsubishi Petrochemical Co., Ltd. | Process for producing ether compounds by catalytic hydrogenolysis |
| US4357477A (en) | 1981-10-29 | 1982-11-02 | Texaco Inc. | Process for preparing ethylene glycol monoalkyl ethers |
| US4356327A (en) | 1981-10-29 | 1982-10-26 | Texaco Inc. | Process for preparing propylene glycol monoalkyl ethers and alkoxyacetones |
| US4390734A (en) | 1982-01-13 | 1983-06-28 | Texaco Inc. | Process for producing propylene glycol monoalkyl ethers from acetaldehyde, an alkanol and syngas using a new catalyst system |
| US4430253A (en) | 1982-02-11 | 1984-02-07 | Ethyl Corporation | Sulfide-modified ruthenium catalyst |
| US4375394A (en) | 1982-03-11 | 1983-03-01 | Eastman Kodak Company | Electrolytic process for the preparation of ethylene glycol and glycerine |
| FR2525211A1 (en) | 1982-04-20 | 1983-10-21 | Ugine Kuhlmann | PROCESS FOR THE PRODUCTION OF MONOETHYLENEGLYCOL MONO-ETHER BY HYDROGENOLYSIS OF CYCLIC ACETALS |
| US4435595A (en) | 1982-04-26 | 1984-03-06 | Eastman Kodak Company | Reactive distillation process for the production of methyl acetate |
| JPS58198431A (en) | 1982-05-12 | 1983-11-18 | Mitsubishi Gas Chem Co Inc | Preparation of 2-alkoxy-alcohol |
| US4482753A (en) | 1983-03-28 | 1984-11-13 | Olin Corporation | Catalyst for use in the hydrogenolysis of methyl glycol formals |
| US4478017A (en) | 1983-03-28 | 1984-10-23 | Brown William R | Flooring protection system |
| DE3328561A1 (en) | 1983-08-08 | 1985-02-28 | Chemische Werke Hüls AG, 4370 Marl | ALIPHATIC MONOETHER OF THE 2.2-DIMETHYLPROPANE-1.3-DIOL WITH C (DOWN ARROW) 3 (DOWN ARROW) - TO C (DOWN ARROW) 2 (DOWN ARROW) (DOWN ARROW) 0 (DOWN ARROW ALUMINUM OXYGEN, 3 -PROPOXY-2.2-DIMETHYLPROPAN-1-OL AND THE 3-TERT.-BUTOXY-2.2-DIMETHYLPROPAN-1-OL, METHOD FOR THE PRODUCTION THEREOF AND THEIR USE AS SOFTENER ALCOHOLS |
| EP0168989A1 (en) | 1984-06-21 | 1986-01-22 | Sun Refining and Marketing Company | Rutheniumpromoted cobalt catalysts for the dealkoxyhydroxymethylation of formaldehyde acetals to form glycol ethers |
| US4692426A (en) | 1984-06-21 | 1987-09-08 | Sun Refining And Marketing Company | Phosphite-promoted ruthenium-cobalt catalysts for the dealkoxyhydroxymethylation of acetals to form glycol ethers |
| US4617287A (en) | 1984-06-21 | 1986-10-14 | Sun Refining And Marketing Company | Ruthenium-cobalt carbonyl catalysts for the dealkoxyhydroxymethylation of aldehyde acetals to form glycol ethers |
| US4652542A (en) | 1984-06-21 | 1987-03-24 | Sun Refining And Marketing Company | Ruthenium-cobalt carbonyl catalysts for the dealkoxyhydroxymethylation of acetals to form glycol ethers |
| EP0169666B1 (en) | 1984-06-21 | 1988-01-27 | Sun Refining and Marketing Company | Catalysts and process for the dealkoxyhydroxymethylation of acetals to form glycol ethers |
| US4618729A (en) | 1984-06-21 | 1986-10-21 | Sun Refining And Marketing Company | Ruthenium-cobalt carbonyl metal cluster catalysts for the dealkoxyhydroxymethylation of acetals to form glycol ethers |
| CA1254190A (en) | 1984-06-21 | 1989-05-16 | James E. Lyons | Ruthenium-promoted cobalt catalysts for the dealkoxyhydroxymethylation of formaldehyde acetals to form glycol ethers |
| US4568780A (en) | 1984-10-22 | 1986-02-04 | Texaco Inc. | Process for low pressure synthesis of ethylene glycol from synthesis gas plus 1,3-dioxolane |
| DD238232A1 (en) | 1985-06-11 | 1986-08-13 | Univ Schiller Jena | PROCESS FOR PREPARING 2,2-DIMETHYL-4-METHYLOL-1,3-DIOXOLANE |
| US4895987A (en) | 1986-06-06 | 1990-01-23 | Sun Refining And Marketing Company | Phosphonite-and phosphonite-promoted ruthenium - cobalt catalysts for the dealkoxyhydroxymethylation of acetals to form glycol ethers |
| JPS63146838A (en) | 1986-12-11 | 1988-06-18 | Japan Tobacco Inc | Acetalization of aldehyde for ketone |
| DE3718564A1 (en) | 1987-06-03 | 1988-12-15 | Basf Ag | METHOD FOR PRODUCING 4-ISOPROPYL-CYCLOHEXYLMETHANOL OR WHOSE ALKYLETHERS |
| JPH01102039A (en) | 1987-10-20 | 1989-04-19 | Sun Refining & Marketing Co | Phosphonite for dealkoxyhydroxymethylating acetal for production of glycol ether and ruthenium cobalt catalyst for phosphonite promotion |
| US4939294A (en) | 1989-05-22 | 1990-07-03 | Eastman Kodak Company | Preparation of ultra high purity methyl acetate |
| DE4104417A1 (en) | 1991-02-14 | 1992-08-20 | Basf Ag | METHOD FOR THE PRODUCTION OF CENTRAL CAMECHIN MONOETHERS AND CENTRAL CYCLES |
| DE69314846T2 (en) | 1992-04-24 | 1998-04-02 | Showa Denko Kk | Process for the preparation of acetaldehyde dimethyl acetal |
| ES2247745T3 (en) | 1992-06-04 | 2006-03-01 | Idemitsu Kosan Co., Ltd. | POLY COMPOUND (VINYL ETER) AND PREPARATION PROCEDURE. |
| JP2841261B2 (en) | 1993-03-15 | 1998-12-24 | 花王株式会社 | Method for producing ether alcohols |
| EP0624563A1 (en) | 1993-05-13 | 1994-11-17 | Kao Corporation | Glycerin derivatives and process for producing the same |
| US5616736A (en) | 1994-02-04 | 1997-04-01 | Hoechst Celanese Corporation | Method of preparing cyclic formals |
| JP3474252B2 (en) * | 1994-02-10 | 2003-12-08 | ポリプラスチックス株式会社 | Method for producing cyclic formal |
| US5720895A (en) | 1994-08-11 | 1998-02-24 | Kao Corporation | Polyol ether derivatives and production methods therefor |
| CN1112342C (en) | 1995-04-20 | 2003-06-25 | 出光兴产株式会社 | Method for producing ether compound |
| US5763691A (en) | 1995-11-30 | 1998-06-09 | Mitsubishi Chemical Corporation | Ethylene glycol process |
| AU692723B2 (en) | 1996-02-01 | 1998-06-11 | Phillips Petroleum Company | Catalyst composition and process for selecting hydrogenation of diolefins |
| US5935896A (en) | 1996-05-02 | 1999-08-10 | Basf Aktiengesellschaft | Catalyst supports and catalysts for dehydrocyanation reactions and processes for producing them |
| DE19621703A1 (en) | 1996-05-30 | 1997-12-04 | Hoechst Ag | Process for the preparation of 3-oxyalkylpropan-1-ols |
| EP0930311B1 (en) | 1996-09-10 | 2003-11-26 | Daiso Co., Ltd. | Process for preparing 1,3-dioxolane-4-methanol compounds |
| JP3296824B2 (en) | 1996-09-10 | 2002-07-02 | ダイソー株式会社 | Method for producing 1,3-dioxolan-4-methanol compound |
| ID21487A (en) | 1996-11-13 | 1999-06-17 | Du Pont | METHOD OF MAKING 1,3 - PROPANDIOL WITH RECOMBINANT ORGANISM |
| DE19648960A1 (en) | 1996-11-26 | 1998-05-28 | Basf Ag | Cyclic acetal or ketal preparation from poly:ol and aldehyde or ketone |
| SG65045A1 (en) | 1997-01-29 | 1999-05-25 | Toray Industries | A method for continuously producing a cyclic formal |
| BE1014031A3 (en) | 1997-07-04 | 2003-03-04 | Basf Ag | THE PREPARATION OF ESTERS. |
| DE19730308A1 (en) | 1997-07-15 | 1999-01-21 | Basf Ag | Process for the preparation of catechol monoethers and catechols |
| AU749910B2 (en) | 1998-03-19 | 2002-07-04 | Mitsubishi Chemical Corporation | Method for producing monoethylene glycol |
| ATE239691T1 (en) | 1998-03-25 | 2003-05-15 | Sulzer Chemtech Ag | METHOD AND DEVICE FOR PRODUCING BUTYL ACETATE AND ISOBUTYL ACETATE |
| US6015875A (en) | 1998-08-11 | 2000-01-18 | Catalytic Distillation Technologies | Process for making acetals |
| DE19840277A1 (en) | 1998-09-04 | 2000-03-09 | Degussa | Process for reducing the content of acetals or ketals in alcoholic reaction mixtures |
| DE19840276C2 (en) | 1998-09-04 | 2002-10-31 | Perstorp Specialty Chem Ab | Process for reducing cleavage of linear and cyclic acetals, especially formals |
| JP2001031671A (en) | 1999-07-15 | 2001-02-06 | Kao Corp | Production of ether acetal |
| JP4287546B2 (en) | 1999-07-27 | 2009-07-01 | 花王株式会社 | Manufacturing method of glyceryl ether |
| JP2001072636A (en) | 1999-09-03 | 2001-03-21 | Kao Corp | Production polyol alkyl ether |
| US6417136B2 (en) | 1999-09-17 | 2002-07-09 | Phillips Petroleum Company | Hydrocarbon hydrogenation catalyst and process |
| JP3802314B2 (en) | 1999-11-02 | 2006-07-26 | 花王株式会社 | Ether production |
| US6207850B1 (en) | 1999-11-03 | 2001-03-27 | Mobil Oil Corporation | Process for co-production of dialkyl carbonate and alkanediol |
| JP3659109B2 (en) | 2000-01-19 | 2005-06-15 | 三菱化学株式会社 | Co-production method of ethylene glycol and carbonate |
| US6166240A (en) | 2000-02-22 | 2000-12-26 | Mobil Oil Corporation | Process for co-production of dialkyl carbonate and alkanediol |
| US6291725B1 (en) | 2000-03-03 | 2001-09-18 | Board Of Trustees Operating Michigan State University | Catalysts and process for hydrogenolysis of sugar alcohols to polyols |
| DE10044352A1 (en) | 2000-09-07 | 2002-03-21 | Basf Ag | Continuous process for the production of acetals |
| IL154960A0 (en) | 2000-10-10 | 2003-10-31 | Du Pont | Polymers having attached luminescent metal complexes and devices made with sych polymers |
| DE10062814A1 (en) | 2000-12-15 | 2002-06-20 | Ticona Gmbh | Process for removing methanol from formaldehyde-containing solutions |
| US6670489B2 (en) | 2001-01-15 | 2003-12-30 | Asahi Kasei Kabushiki Kaisha | Process for producing cyclic formal |
| US6548681B1 (en) | 2001-06-26 | 2003-04-15 | Board Of Trustees Of Michigan State University | Process for the recovery of a polyol from an aqueous solution |
| US6930206B1 (en) | 2001-07-05 | 2005-08-16 | Catalytic Distillation Technologies | Process and apparatus for catalytic distillations |
| US6969779B2 (en) | 2002-11-01 | 2005-11-29 | Shell Oil Company | Method for removal of MW176 cyclic acetal formed during the production of 1,3-propanediol |
| DE10255647A1 (en) | 2002-11-28 | 2004-06-09 | Basf Ag | Process for obtaining an aliphatic dialdehyde monoacetal |
| EP1510512B1 (en) | 2003-08-27 | 2014-12-31 | Mitsubishi Gas Chemical Company, Inc. | Process for producing alicyclic aldehydes |
| PT103123A (en) | 2004-05-19 | 2005-11-30 | Univ Do Porto | INDUSTRIAL PROCESS OF ACETAL PRODUCTION IN AN ADSORPTIVE REACTOR OF SIMULATED MOVEL MOBILE |
| US7534922B2 (en) | 2004-12-13 | 2009-05-19 | Ticona Gmbh | Processes for the manufacture of acetals |
| EP1861483A4 (en) | 2005-03-01 | 2009-04-01 | Univ Michigan State | Process for production of a composition useful as a fuel |
| DE102005042505A1 (en) | 2005-09-07 | 2007-03-08 | Basf Ag | Process for the preparation of dioxolane |
| DE102005051974A1 (en) | 2005-10-31 | 2007-05-03 | Basf Ag | Preparing trioxane and comonomer, useful for preparing trioxane based (co)polymer, comprises converting formaldehyde and co-monomer educt to trioxane and co-monomer, and distillating the obtained reaction mixtures |
| FR2906246B1 (en) | 2006-09-22 | 2008-12-12 | Arkema France | PROCESS FOR SYNTHESIZING CYCLIC ACETALS IN A SIMUL MOBILE BED REACTOR |
| FR2906807A1 (en) | 2006-10-09 | 2008-04-11 | Arkema France | PROCESS FOR THE SYNTHESIS OF CYCLIC ACETALS BY REACTIVE EXTRACTION OF A POLYOL IN A CONCENTRATED SOLUTION |
| CA2668294C (en) | 2007-10-09 | 2010-12-07 | Segetis, Inc. | Method of making ketals and acetals |
| JP5209941B2 (en) | 2007-11-13 | 2013-06-12 | 昭和電工株式会社 | Method for producing α, β-unsaturated ether |
| DE102008002347A1 (en) | 2008-06-11 | 2009-12-17 | Evonik Oxeno Gmbh | Catalyst and process for the preparation of saturated ethers by hydrogenation of unsaturated ethers |
| CN107082742A (en) | 2008-08-25 | 2017-08-22 | 陶氏环球技术有限责任公司 | Polyol ethers and the method for preparing them |
| US7981390B2 (en) | 2008-12-23 | 2011-07-19 | Basf Corporation | Small engine palladium catalyst article and method of making |
| US8633127B2 (en) | 2009-03-04 | 2014-01-21 | Chevron Phillips Chemical Company Lp | Selective hydrogenation catalyst and methods of making and using same |
| WO2011106194A2 (en) | 2010-02-23 | 2011-09-01 | Dow Global Technologies Llc | Process for making polyol ethers |
| EP2638037A4 (en) | 2010-11-11 | 2015-02-18 | Segetis Inc | Polyhydroxy ketal ester adducts, methods of manufacture and uses thereof |
| US9388105B2 (en) | 2011-06-24 | 2016-07-12 | Eastman Chemical Company | Production of hydroxy ether hydrocarbons by liquid phase hydrogenolysis of cyclic acetals or cyclic ketals |
| US9056313B2 (en) | 2011-06-24 | 2015-06-16 | Eastman Chemical Company | Catalysts for the production of hydroxy ether hydrocarbons by vapor phase hydrogenolysis of cyclic acetals and ketals |
| US9000229B2 (en) | 2011-06-24 | 2015-04-07 | Eastman Chemical Company | Production of hydroxy ether hydrocarbons by vapor phase hydrogenolysis of cyclic acetals and ketals |
| US8829207B2 (en) | 2011-06-24 | 2014-09-09 | Eastman Chemical Company | Production of cyclic acetals by reactive distillation |
| US8785697B2 (en) | 2011-06-24 | 2014-07-22 | Eastman Chemical Company | Nickel modified catalyst for the production of hydroxy ether hydrocarbons by vapor phase hydrogenolysis of cyclic acetals and ketals |
| US8829206B2 (en) | 2011-06-24 | 2014-09-09 | Eastman Chemical Company | Production of cyclic acetals or ketals using solid acid catalysts |
| US8969598B2 (en) | 2011-06-24 | 2015-03-03 | Eastman Chemical Company | Production of cyclic acetals or ketals using liquid-phase acid catalysts |
-
2011
- 2011-06-24 US US13/168,374 patent/US8969598B2/en active Active
-
2012
- 2012-06-14 CN CN201280030098.4A patent/CN103619830B/en active Active
- 2012-06-14 WO PCT/US2012/042458 patent/WO2012177485A1/en active Application Filing
-
2015
- 2015-01-26 US US14/605,067 patent/US9394271B2/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5446210A (en) * | 1991-07-20 | 1995-08-29 | Henkel Kommanditgesellschaft Auf Aktien | Process for the production of polyol ethers |
| US5917059A (en) * | 1996-11-15 | 1999-06-29 | Basf Aktiengesellschaft | Preparation of cyclic acetals or ketals |
Also Published As
| Publication number | Publication date |
|---|---|
| US20150141668A1 (en) | 2015-05-21 |
| US8969598B2 (en) | 2015-03-03 |
| US9394271B2 (en) | 2016-07-19 |
| CN103619830A (en) | 2014-03-05 |
| US20120330033A1 (en) | 2012-12-27 |
| WO2012177485A1 (en) | 2012-12-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103619830B (en) | Liquid phase acid catalyst is used to manufacture cyclic acetal or ketal | |
| CN103619829B (en) | Solid acid catalyst is used to manufacture cyclic acetal or ketal | |
| US9315485B2 (en) | Production of cyclic acetals by reactive distillation | |
| JP5757934B2 (en) | Process for producing α, β-unsaturated C10 aldehyde | |
| CN103130611B (en) | Neopentyl glycol condensation hydrogenation production technique and device thereof | |
| TWI450883B (en) | Process for preparing polymethylols | |
| CN101641315A (en) | Manufacture of purified alcohols | |
| CN104080760A (en) | Apparatus and method for preparing alcohol from olefin | |
| JP2009513687A (en) | Process for the production of trioxane and at least one comonomer | |
| KR20160039215A (en) | Alkylene oxide separation systems, methods, and apparatuses | |
| CN101589015B (en) | Method for the production of acrylic acid | |
| KR101808248B1 (en) | A continuous process for preparing neopentyl glycol | |
| JP4245921B2 (en) | Method for producing cyclic formal | |
| TW200906777A (en) | Reducing heavy byproduct formtion during recovery of dichlorohydrins | |
| CN103562192B (en) | Method with extraction distillation column separation oxyalkylene | |
| CN101389590A (en) | Process for the preparation of an alkanediol and a dialkyl carbonate | |
| JP5868413B2 (en) | Method for producing 1,3,5-trioxane | |
| US20140107380A1 (en) | Method for producing bioderived dipropylene and tripropylene glycols without propylene oxide | |
| CN104024200B (en) | The method being recovered by distillation double-trimethylolpropane | |
| RU2255936C1 (en) | Method for preparing 4,4-dimethyl-1,3-dioxane | |
| TWI486325B (en) | Recovery of trimethylolpropane from purification residue | |
| RU2036919C1 (en) | Method of 1,3-dioxolane synthesis | |
| JP2001158781A (en) | 4-methylene-1,3-dioxolane containing functional group and method for producing the same | |
| CN101668754A (en) | Method for producing trioxane from trioxymethylene glycol dimethyl ether |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |